Method and catalyst system for producing aromatic carbonates

ABSTRACT

A method and catalyst system for producing aromatic carbonates from aromatic hydroxy compounds. In one embodiment, the method includes the step of contacting at least one aromatic hydroxy compound with oxygen and carbon monoxide in the presence of a carbonylation catalyst system having catalytic amounts of the following components: a Group VIII B metal source; a combination of inorganic co-catalysts including a copper source and at least one of a titanium source or a zirconium source; an onium chloride composition; and a base. Alternative embodiments include inorganic co-catalyst combinations of a lead source and at least one of a titanium source or a manganese source.

This application is a division of application Ser. No. 09/495,539, filedJan. 31, 2000, now U.S. Pat. No. 6,207,849, which is hereby incorporatedby reference in its entirety.

BACKGROUND

1. Field of the Invention

The present invention is directed to a method and catalyst system forproducing aromatic carbonates and, more specifically, to a method andcatalyst system for producing diaryl carbonates through thecarbonylation of aromatic hydroxy compounds.

2. Discussion of Related Art

Aromatic carbonates find utility, inter alia, as intermediates in thepreparation of polycarbonates. For example, a popular method ofpolycarbonate preparation is the melt transesterification of aromaticcarbonates with bisphenols. This method has been shown to beenvironmentally superior to previously used methods which employedphosgene, a toxic gas, as a reagent and chlorinated aliphatichydrocarbons, such as methylene chloride, as solvents.

Various methods for preparing aromatic carbonates have been previouslydescribed in the literature and/or utilized by industry. A method thathas enjoyed substantial popularity in the literature involves the directcarbonylation of aromatic hydroxy compounds with carbon monoxide andoxygen. In general, practitioners have found that the carbonylationreaction requires a rather complex catalyst system. For example, in U.S.Pat. No. 4,187,242, which is assigned to the assignee of the presentinvention, Chalk reports that a carbonylation catalyst system shouldcontain a Group VIII B metal, such as ruthenium, rhodium, palladium,osmium, iridium, platinum, or a complex thereof. Further refinements tothe carbonylation reaction include the identification of organicco-catalysts, such as terpyridines, phenanthrolines, quinolines andisoquinolines in U.S. Pat. No. 5,284,964 and the use of certain halidecompounds, such as quaternary ammonium or phosphonium halides in U.S.Pat. No. 5,399,734, both patents also being assigned to the assignee ofthe present invention.

The economics of the carbonylation process is strongly dependent on thenumber of moles of aromatic carbonate produced per mole of Group VIII Bmetal utilized (i.e. “catalyst turnover”). Consequently, much work hasbeen directed to the identification of efficacious catalyst combinationsthat increase catalyst turnover. In U.S. Pat. No. 5,231,210, which isalso assigned to the present assignee, Joyce et al. report the use of acobalt pentadentate complex as an inorganic co-catalyst (“IOCC”). InU.S. Pat. No. 5,498,789, Takagi et al. report the use of lead as anIOCC. In U.S. Pat. No. 5,543,547, Iwane et al. report the use oftrivalent cerium as an IOCC. In U.S. Pat. No. 5,726,340, Takagi et al.report the use of lead and cobalt as a binary IOCC system.

Carbonylation catalyst literature lauds the effectiveness of bromidecompounds as a halide source in the catalyst system. For example, in theaforementioned U.S. Pat. No. 5,543,547, Iwane et al. state thetraditional understanding that bromide sources are the preferred halidesources and that chloride is known to exhibit low activity. While it istrue that bromide has historically exhibited higher activity, there aredrawbacks to using bromide in the carbonylation reaction. Initially, itis worth noting that onium bromide compounds are typically expensivecompared to, e.g., onium chloride compounds. Furthermore, when used tocarbonylate phenol, bromide ion is consumed in the process formingundesirable brominated byproducts, such as 2- and 4- bromophenols andbromo diphenylcarbonate. These byproducts must typically be recoveredand recycled, further adding to the investment and operating cost of theprocess. However, due to their comparatively low activity, oniumchloride compounds have not traditionally been considered aneconomically viable alternative to onium bromide compounds.

Unfortunately, the literature is not instructive regarding the role ofmany catalyst components in the carbonylation reaction (i.e. thereaction mechanism). Accordingly, meaningful guidance regarding theidentification of effective combinations of catalyst system componentsis cursory at best. In this regard, periodic table groupings have failedto provide guidance in identifying additional IOCC's. For example, U.S.Pat. No. 5,856,554 provides a general listing of possible IOCCcandidates, yet further analysis has revealed that many of the members(and combinations of members) of the recited groups (i.e., Groups IV Band V B) do not effectively catalyze the carbonylation reaction.Therefore, due to the lack of guidance in the literature, theidentification of effective carbonylation catalyst systems has become aserendipitous exercise.

As the demand for high performance plastics has continued to grow, newand improved methods of providing product more economically are neededto supply the market. In this context, various processes and catalystsystems are constantly being evaluated; however, the identities ofimproved and/or additional effective catalyst systems for theseprocesses continue to elude the industry. Consequently, a long felt, yetunsatisfied need exists for new and improved methods and catalystsystems for producing aromatic carbonates and the like.

SUMMARY OF THE INVENTION

Accordingly, the present invention is directed to a method and catalystsystem for producing aromatic carbonates. In one embodiment, the methodincludes the step of contacting at least one aromatic hydroxy compoundwith oxygen and carbon monoxide in the presence of a carbonylationcatalyst system having catalytic amounts of the following components: aGroup VIII B metal source; a combination of inorganic co-catalystsincluding a copper source and at least one of a titanium source or azirconium source; an onium chloride composition; and a base.

In various alternative embodiments, the carbonylation catalyst systemcan include catalytic amounts inorganic co-catalyst combinations of alead source and at least one of a titanium source or a manganese source.

BRIEF DESCRIPTION OF THE DRAWING

Various features, aspects, and advantages of the present invention willbecome more apparent with reference to the following description,appended claims, and accompanying drawing, wherein the FIGURE is aschematic view of a device capable of performing an aspect of anembodiment of the present invention.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

The present invention is directed to a method and catalyst system forproducing aromatic carbonates. In one embodiment, the method includesthe step of contacting at least one aromatic hydroxy compound withoxygen and carbon monoxide in the presence of a carbonylation catalystsystem having catalytic amounts of the following components: a GroupVIII B metal source; a combination of inorganic co-catalysts; an oniumchloride composition; and a base.

For convenience, the constituents of the catalyst system describedherein are called “components” irrespective of whether a reactionbetween specific components actually occurs either before or during thecarbonylation reaction. Therefore, the catalyst system may include thecomponents and any reaction products thereof.

Unless otherwise noted, the term “catalytic amount,” as used herein,includes that amount of a component capable of either increasing(directly or indirectly) the yield of the carbonylation product orincreasing selectivity toward an aromatic carbonate. Optimum amounts ofa given component can vary based on reaction conditions and the identityof other components, yet can be readily determined in light of thediscrete circumstances of a given application.

Aromatic hydroxy compounds which may be used in the present processinclude aromatic mono or polyhydroxy compounds, such as phenol, cresol,xylenol, resorcinol, hydroquinone, and bisphenol A. Aromatic organicmono hydroxy compounds are preferred, with phenol being more preferred.

In various preferred embodiments, the carbonylation catalyst systemcontains at least one constituent from the Group VIII B metals or acompound thereof. A preferred Group VIII B constituent is a catalyticamount of a palladium source. The palladium source may be anon-supported Pd(II) salt or complex. As used herein, the term“non-supported” indicates the absence of industrially conventionalcatalyst supports based on carbon, element oxides, element carbides orelement salts in various presentations. Examples of supports containingcarbon are coke, graphite, carbon black and activated carbon. Examplesof element oxide catalyst supports are SiO₂ (natural or syntheticsilicas, quartz), Al₂O₃ (α-, γ- Al₂O₃), aluminas, natural and syntheticaluminosilicates (zeolites), TiO₂ (rutile, anatase), ZrO₂ and ZnO.Examples of element carbides and salts are SiC, AlPO₄, BaSO₄, and CaCO₃.

Accordingly, suitable palladium sources include palladium halides,nitrates, carboxylates, oxides and palladium complexes containing carbonmonoxide, amines, phosphines or olefins. As used herein, the term“complex” includes coordination or complex compounds containing acentral ion or atom. The complexes may be nonionic, cationic, oranionic, depending on the charges carried by the central atom and thecoordinated groups. Other common names for these complexes includecomplex ions (if electrically charged), Werner complexes, andcoordination complexes.

In various applications, it may be preferable to utilize palladium(II)salts of organic acids, including carboxylates with C₂₋₆ aliphaticacids. Palladium(II) acetylacetonate anddichloro(1,4-bis(diphenylphosphino)butane) palladium (II) are alsosuitable palladium sources. Preferably, the amount of Group VIII B metalsource employed should be sufficient to provide about 1 mole of metalper 800-10,000 moles of aromatic hydroxy compound. More preferably, theproportion of Group VIII B metal source employed should be sufficient toprovide about 1 mole of metal per 2,000-5,000 moles of aromatic hydroxycompound.

The carbonylation catalyst system further contains a catalytic amount ofan onium chloride composition, such as an organic onium chloride salt.The salt may be a quaternary ammonium or phosphonium chloride salt, or ahexaalkylguanidinium chloride salt. In various embodiments, α,ω-bis(pentaalkylguanidinium)alkane chloride salts may be preferred.Suitable onium chloride compositions include tetrabutylammoniumchloride, tetraethylammonium chloride, and hexaethylguanidiniumchloride. In preferred embodiments, the carbonylation catalyst systemcan contain between about 5 and about 2000 moles of chloride per mole ofpalladium employed, and, more preferably, between about 50 and about1000 molar equivalents of chloride are used.

The carbonylation catalyst system also includes a catalytic amount of abase. Any desired bases or mixtures thereof, whether organic orinorganic may be used. A non-exclusive listing of suitable inorganicbases include alkali metal hydroxides and carbonates; C₂-C₁₂carboxylates or other salts of weak acids; and various alkali metalsalts of aromatic hydroxy compounds, such as alkali metal phenolates.Hydrates of alkali metal phenolates may also be used. Examples ofsuitable organic bases include tertiary amines and the like. Preferably,the base used is an alkali metal salt incorporating an aromatic hydroxycompound, more preferably an alkali metal salt incorporating thearomatic hydroxy compound to be carbonylated to produce the aromaticcarbonate. A preferred base is sodium phenoxide. In preferredembodiments, between about 5 and about 1000 molar equivalents of baseare employed (relative to palladium), and, more preferably, betweenabout 100 and about 700 molar equivalents of base are used.

The carbonylation catalyst system includes a catalytic amount of acombination of inorganic co-catalysts (IOCC's). It has been discoveredthat certain IOCC combinations can effectively catalyze thecarbonylation reaction in the presence of the aforementioned catalystsystem components. Such IOCC combinations include lead and titanium;lead and manganese; copper and titanium; and copper and zirconium.Additional IOCC's may be used in the carbonylation catalyst system,provided the additional IOCC does not deactivate (i.e. “poison”) theoriginal IOCC combination. Examples of additional IOCC's include zincand cerium.

An IOCC can be introduced to the carbonylation reaction in variousforms, including salts and complexes, such as tetradentate,pentadentate, hexadentate, or octadentate complexes. Illustrative formsmay include oxides, halides, carboxylates, diketones (includingbeta-diketones), nitrates, complexes containing carbon monoxide orolefins, and the like. Suitable beta-diketones include those known inthe art as ligands for the IOCC metals of the present system. Examplesinclude, but are not limited to, acetylacetone, benzoylacetone,dibenzoylmethane, diisobutyrylmethane, 2,2-dimethylheptane-3,5-dione,2,2,6-trimethylheptane-3,5-dione, dipivaloylmethane, andtetramethylheptanedione. The quantity of ligand is preferably not suchthat it interferes with the carbonylation reaction itself, with theisolation or purification of the product mixture, or with the recoveryand reuse of catalyst components (such as palladium). An IOCC may beused in its elemental form if sufficient reactive surface area can beprovided. However, it is preferable that an IOCC is non-supported asdiscussed above relative to the Group VII B metals.

IOCC's are included in the carbonylation catalyst system in catalyticamounts. In this context a “catalytic amount” is an amount of IOCC (orcombination of IOCC's) that increases the number of moles of aromaticcarbonate produced per mole of Group VIII B metal utilized; increasesthe number of moles of aromatic carbonate produced per mole of chlorideutilized; or increases selectivity toward aromatic carbonate productionbeyond that obtained in the absence of the IOCC (or combination ofIOCC's). Optimum amounts of an IOCC in a given application will dependon various factors, such as the identity of reactants and reactionconditions. For example, when palladium is included in the reaction, themolar ratio of copper relative to palladium at the initiation of thereaction is preferably between about 0.1 and about 100.

The carbonylation reaction can be carried out in a batch reactor or acontinuous reactor system. Due in part to the low solubility of carbonmonoxide in organic hydroxy compounds, such as phenol, it is preferablethat the reactor vessel be pressurized. In preferred embodiments, gascan be supplied to the reactor vessel in proportions of between about 2and about 50 mole percent oxygen, with the balance being carbon monoxideand, in any event, outside the explosion range for safety reasons. It iscontemplated that oxygen can be supplied in diatomic form or fromanother oxygen containing source, such as peroxides and the like.Additional gases may be present in amounts that do not deleteriouslyaffect the carbonylation reaction. The gases may be introducedseparately or as a mixture. A total pressure in the range of betweenabout 10 and about 250 atmospheres is preferred. Drying agents,typically molecular sieves, may be present in the reaction vessel.Reaction temperatures in the range of between about 60° C. and about150° C. are preferred. Gas sparging or mixing can be used to aid thereaction.

In order that those skilled in the art will be better able to practicethe present invention reference is made to the FIGURE, which shows anexample of a continuous reactor system for producing aromaticcarbonates. The symbol “V” indicates a valve and the symbol “P”indicates a pressure gauge.

The system includes a carbon monoxide gas inlet 10, an oxygen inlet 11,a manifold vent 12, and an inlet 13 for a gas, such as carbon dioxide. Areaction mixture can be fed into a low pressure reservoir 20, or a highpressure reservoir 21, which can be operated at a higher pressure thanthe reactor for the duration of the reaction. The system furtherincludes a reservoir outlet 22 and a reservoir inlet 23. The gas feedpressure can be adjusted to a value greater than the desired reactorpressure with a pressure regulator 30. The gas can be purified in ascrubber 31 and then fed into a mass flow controller 32 to regulate flowrates. The reactor feed gas can be heated in a heat exchanger 33 havingappropriate conduit prior to being introduced to a reaction vessel 40.The reaction vessel pressure can be controlled by a back pressureregulator 41. After passing through a condenser 25, the reactor gaseffluent may be either sampled for further analysis at valve 42 orvented to the atmosphere at valve 50. The reactor liquid can be sampledat valve 43. An additional valve 44 can provide further system control,but is typically closed during the gas flow reaction.

In the practice of one embodiment of the invention, the carbonylationcatalyst system and aromatic hydroxy compound are charged to the reactorsystem. The system is sealed. Carbon monoxide and oxygen are introducedinto an appropriate reservoir until a preferred pressure (as previouslydefined) is achieved. Circulation of condenser water is initiated, andthe temperature of the heat exchanger 33 (e.g., oil bath) can be raisedto a desired operating temperature. A conduit 46 between heat exchanger33 and reaction vessel 40 can be heated to maintain the desiredoperating temperature. The pressure in reaction vessel 40 can becontrolled by the combination of reducing pressure regulator 30 and backpressure regulator 41. Upon reaching the desired reactor temperature,aliquots can be taken to monitor the reaction.

EXAMPLES

The following examples are included to provide additional guidance tothose skilled in the art in practicing the claimed invention. While someof the examples are illustrative of various embodiments of the claimedinvention, others are comparative and are identified as such. Theexamples provided are merely representative of the work that contributesto the teaching of the present application. Accordingly, these examplesare not intended to limit the invention, as defined in the appendedclaims, in any manner. Unless otherwise specified, all parts are byweight, and all equivalents are relative to palladium. Reaction productswere verified by gas chromatography. All reactions were carried out in aglass, batch reactor at 100° C. in an approximately 6-7% O₂ in COatmosphere at an operating pressure of 108.9 atm. Reaction time was 3hours for each run. Each reaction was run in replicate (3x or 4x) withthe average of the replicate runs reported herein.

As discussed supra, the economics of aromatic carbonate production isdependent on the number of moles of aromatic carbonate produced per moleof Group VIII B metal utilized. In the following examples, the aromaticcarbonate produced is diphenylcarbonate (DPC) and the Group VIII B metalutilized is palladium. For convenience, the number of moles of DPCproduced per mole of palladium utilized is referred to as the palladiumturnover number (Pd TON). Various preferred embodiments of the presentmethod produce Pd TON of at least 1500. Even more preferred embodimentsproduce Pd TON of at least 2500.

Example 1

Diphenyl carbonate was produced by adding, at ambient conditions, 0.25mM dichloro(1,4-bis(diphenylphosphino)butane) palladium(II)[“Pd(dppb)Cl₂”], 600 equivalents of chloride in the form oftetrabutylammonium chloride (“TBAC”), 150 equivalents of phenoxide inthe form of sodium phenoxide (“NaOPh”), and an IOCC combination of leadand titanium in various amounts to a glass reaction vessel containingphenol. Lead was supplied as lead (II) oxide (“PbO”) and titanium astitanium(IV) oxide acetylacetonate (“TiO(acac)₂”). The components wereheated to 100° C. for 3 hours in an approximately 6-7% oxygen in carbonmonoxide atmosphere. The following results were observed:

Experiment Pd (dppb) Cl₂ PbO TiO (acac)₂ No. mM Equivalents EquivalentsPd TON 1 .25 24 5.6 1847 2 .25 50 5.6 2124

The various reaction conditions show that a Pd TON at least as high as2124 can be obtained utilizing this catalyst system. Based on theresults of these experiments, it is evident that a catalyst systemcontaining Pd, a base, an onium chloride, Pb, and Ti can effectivelycatalyze the carbonylation reaction.

Example 2

The general procedure of Example 1 was repeated with 0.25 mMPd(dppb)Cl₂, 600 equivalents of TBAC, 150 equivalents of NaOPh, and anIOCC combination of 50 equivalents of lead and 5.6 equivalents ofmanganese. Lead was supplied as PbO and manganese as manganese (III)acetylacetonate (“Mn(acac)₃”). The average Pd TON was found to be 2375,thus showing that the combination of Pd, base, onium chloride, Pb, andMn can effectively catalyze the carbonylation reaction.

Example 3

The general procedure of Examples 1 and 2 was repeated with 0.25 mMPd(dppb)Cl₂, 600 equivalents of TBAC, 150 equivalents of NaOPh, and anIOCC combination of 12 equivalents of copper and 5.6 equivalents oftitanium. Copper was supplied as copper (II) acetylacetonate(“Cu(acac)₂”) and titanium as TiO(acac)₂. The average Pd TON was foundto be 4079, thus showing that the combination of Pd, base, oniumchloride, Cu, and Ti can effectively catalyze the carbonylationreaction.

Example 4

The general procedure of Examples 1-3 was repeated with 0.25 mMPd(dppb)Cl₂, 600 equivalents of TBAC, 150 equivalents of NaOPh, and anIOCC combination of 50 equivalents of copper and 12 equivalents ofzirconium. Copper was supplied as Cu(cac)₂ and zirconium as zirconium(IV) butoxide (“Zr(OBu)₄”). The average Pd TON was found to be 2350,thus showing that the combination of Pd, base, onium chloride, Cu, andZr can effectively catalyze the carbonylation reaction.

Comparative Example A

To show the comparative effectiveness of the previously detailedcatalyst systems, replicate runs were conducted using the generalprocedure of Examples 1-4 with the following catalyst system components:0.25 mM Pd(dppb)Cl₂, 600 equivalents of TBAC, and 50 equivalents of PbO.The results are shown below:

Experiment Pd (dppb) Cl₂ PbO NaOPh No. mM Equivalents Equivalents Pd TON1 .25 50 0 497 2 .25 50 150 1623

These results illustrate that the catalyst systems of Examples 1 and 2perform substantially better than the present system with or withoutadded base at the conditions utilized.

Comparative Example B

Replicate runs were conducted using the general procedure of Examples1-4 with the following catalyst system components: 0.25 mM Pd(dppb)Cl₂,600 equivalents of TBAC, and 24 equivalents of Cu(acac)₂. The resultsare shown below:

Experiment Pd (dppb) Cl₂ Cu (acac)₂ NaOPh No. mM Equivalents EquivalentsPd TON 1 .25 24 0 42 2 .25 24 150 957

These results illustrate that the catalyst systems of Examples 3 and 4perform substantially better than the present system with or withoutadded base at the conditions utilized.

It will be understood that each of the elements described above, or twoor more together, may also find utility in applications differing fromthe types described herein. While the invention has been illustrated anddescribed as embodied in a method and catalyst system for producingaromatic carbonates, it is not intended to be limited to the detailsshown, since various modifications and substitutions can be made withoutdeparting in any way from the spirit of the present invention. Forexample, additional effective IOCC compounds can be added to thereaction. As such, further modifications and equivalents of theinvention herein disclosed may occur to persons skilled in the art usingno more than routine experimentation, and all such modifications andequivalents are believed to be within the spirit and scope of theinvention as defined by the following claims.

What is claimed is:
 1. A carbonylation catalyst system, comprising thefollowing components: a Group VIII B metal source; a combination ofinorganic co-catalysts including a lead source and at least one of atitanium source or a manganese source; an onium chloride composition;and a base.
 2. The carbonylation catalyst system of claim 1, wherein theGroup VIII B metal source is a palladium source.
 3. The carbonylationcatalyst system of claim 2, wherein the palladium source is anon-supported Pd(II) salt or complex.
 4. The carbonylation catalystsystem of claim 3, wherein the palladium source isdichloro(1,4-bis(diphenylphosphino)butane) palladium (II).
 5. Thecarbonylation catalyst system of claim 1, wherein the onium chloridecomposition is tetrabutylammonium chloride.
 6. The carbonylationcatalyst system of claim 1, wherein the base is sodium phenoxide.
 7. Thecarbonylation catalyst system of claim 1, wherein the combination ofinorganic co-catalysts includes a lead source and a titanium source. 8.The carbonylation catalyst system of claim 1, wherein the combination ofinorganic co-catalysts includes a lead source and a manganese source. 9.A carbonylation catalyst system, comprising the following components: aGroup VIII B metal source; a combination of inorganic co-catalystsincluding a copper source and at least one of a titanium source or azirconium source; an onium chloride composition; and a base.
 10. Thecarbonylation catalyst system of claim 9, wherein the Group VIII metalsource is a palladium source.
 11. The carbonylation catalyst system ofclaim 10, wherein the palladium source is a non-supported Pd(II) salt orcomplex.
 12. The carbonylation catalyst system of claim 11, wherein thepalladium source is dichloro(1,4-bis(diphenylphosphino)butane) palladium(II).
 13. The carbonylation catalyst system of claim 9, wherein theonium chloride composition is tetrabutylammonium chloride.
 14. Thecarbonylation catalyst system of claim 9, wherein the base is sodiumphenoxide.
 15. The carbonylation catalyst system of claim 9, wherein thecombination of inorganic co-catalysts includes a lead source and atitanium source.
 16. The carbonylation catalyst system of claim 9,wherein the combination of inorganic co-catalysts includes a lead sourceand a zirconium source.